Method for the direct oxidation and/or internal reforming of ethanol, solid oxide fuel cell for direct oxidation and/or internal reforming of ethanol, catalyst and multifunctional electrocatalytic anode for direct oxidation and/or internal

ABSTRACT

The present invention relates to the direct oxidation and/or internal reforming of ethanol and/or mixtures of ethanol and water, in a solid oxide fuel cell, with multifunctional electrocatalytic anodes having specific features, on the basis of mixed oxides and metal oxides and catalysts, preferably with a perovskite-like crystalline structure.

TECHNICAL FIELD

The present invention relates to the direct oxidation and/or internal reforming of ethanol in a solid oxide fuel cell (SOFC) with anode electrocatalysts special functionality that have catalytic or electrocatalytic electrochemical resistance to carbon deposition and selective competitive catalytic action, through chemical reactions that compete with the generation of electrons in electrochemical reactions, the degree of electrocatalytic activity, which influences the electrochemical performance and can facilitate the direct oxidation or reforming complex internal fuel such as ethanol or mixtures ethanol-water at the anode of the fuel cell in order to produce electricity and/or possibly even catalytic conversion/electrocatalytic specific, resulting in the production of ethylene.

Direct Oxidation and/or Internal Reforming of Ethanol in Solid Oxide Fuel Cells

The solid oxide fuel cell (SOFC) are considered promising for the generation of electricity due to its high efficiency, low cost and fuel flexibility. Many fuels have been suggested as potentially applicable for SOFCs and among them, ethanol is presented as very attractive because it is a liquid fuel storage easy and safe, it is renewable and can be produced from various biomass sources, including power plants, contains the OH group, which facilitates the process of direct oxidation and / or internal reform, in addition, ethanol can be easily mixed with the required amount of water and vaporized to generate electricity.

SOFC can operate being fed directly to ethanol without the need for external reform, provided it has functionality specific to this anode. If this condition met, a power generation system with direct feed from ethanol or ethanol-water mixtures in a SOFC can be simple and targeted at portable applications, mobile or stationary. Such a system has the advantages of operating with high efficiency and without the production of pollutants such as NO_(x) and SO_(x), with reduced CO₂ emissions.

For direct oxidation in SOFCs, ethanol is electrochemically oxidized at the electrocatalytic anode, according to the reactions shown as below:

Cathode 3O₂+12e ⁻=6O²⁻

Anode C₂H₅OH+6O²⁻=2CO₂+3H₂O+12e ³¹ (direct oxidation reaction)

total C₂H₅OH+3O₂=2CO₂+3H₂O

Many efforts have been made to understand and make ethanol electrooxidation on anode electrocatalyst surface and define the mechanism of occurrence. The route is desired that oxidizes ethanol directly to CO₂, with the production of 12e⁻, which results in the greatest amount of electrons and, consequently, more energy released.

Alternatively, ethanol can be reformed internally in SOFCs, followed by electrochemical oxidation of hydrogen and carbon monoxide. In this case, the reactions are as follows:

Cathode 3O₂+12e ⁻=6O²⁻

Anode C₂H₅OH+3H₂O=2CO₂+6H₂ (reforming reaction)

C₂H₅OH+H₂O=2CO+4H₂

CO+O⁻²=CO₂+2e ³¹

6H₂+6O²⁻=6H₂O+12e ⁻(electrochemical reaction)

total C₂H₅OH+3O₂=2CO₂+3H₂O

The main mechanisms involve the reactions of dehydration or dehydrogenation of ethanol. The dehydration reaction produces ethylene as an intermediary and water, as shown:

Dehydration::C₂H₅OH=C₂H₄+H₂O

Dehydrogenation::C₂H₅OH=CH₃+CHO+H₂

SOFC operating directly on fuels such as hydrogen, hydrocarbons, ethanol or ethanol-water mixtures generates heat during operation. Douvartzides, S. et al. in “Exergy analysis of a solid oxide fuel cell power plant fed either with ethanol or methane” Journal of Power Sources, V-131, pages 224-230, and in 2004, “Electricity from ethanol fed SOFCs: the expectations for sustainable development and technological benefits” International Journal of Hydrogen Energy, V.29, pages 375-379, 2004, observed that when the SOFC is fed with ethanol achieves a theoretical efficiency in the range 84 to 93%, operating under free carbon between 800 and 1200K. This efficiency classifies ethanol as a fuel option more viable for SOFCs that gasoline and methanol.

Cermet Ni-ZEI (zirconia stabilized with 8 mol % yttria) is the most applied in SOFC anode because it has good activity for oxidation of hydrogen in the cell operating conditions. However, the use of nickel catalysts at the anode of a SOFC fed directly to hydrocarbons and alcohols, resulting in cell degradation due to deposition of carbon. Consequently, the development of anode materials resistant to carbon deposition is an important technological goal. Additionally, in the specific case of ethanol, it is necessary to achieve high anode potential to break the C-C bond, thus promoting the full oxidation of ethanol to CO₂. Gort et al., In “Novel SOFC anodes for the direct electrochemical oxidation of hydrocarbons” Journal of Catalysis V.216, pages 477-486, 2003, reported in their work, for example, that the problem of carbon deposition observed in anodes Ni-based anodes can be avoided by using Cu-ZEI at intermediate temperatures. Copper has high electronic conductivity and low catalytic activity for carbon formation and, therefore, is chosen to replace the nickel. These researchers have focused their attention on developing anodes resistant to carbon deposition of nickel by replacing copper and CeO₂. According to these researchers, “Recent developments on anodes for direct fuel utilization in SOFC”, Solid State Ionics V. 175, pages 1-6, 2004, copper has some limitations, for example, the low catalytic activity for oxidation of hydrocarbon fuels and alcohols. Thus, it is necessary to functionalize the anode through the manufacture of a composite in which the electronic conduction should be ensured by copper and a different material to promote the catalytic activity for fuel oxidation. In this anode, the ceria is added as a catalyst for the oxidation of fuel and also to present mixed conductivity in its reduced form, which allows the transfer of oxygen ions from the electrolyte to the catalytic surface and assists charge transfer processes at the boundary triple phase.

Wen T. L et al. In “Preparation and performance of the Cu—CeO₂—ScSZ composite anode for SOFCs running on ethanol fuel” Journal of power sources V.164, pages 203-209, 2007, have been researching SOFC anodes with Cu—CeO₂—ScSZ (ScSZ which represents zirconia stabilized with scandium) for operation with ethanol. The results obtained by these researchers was very satisfactory, since the maximum power density obtained for SOFCs operated with vaporized ethanol was 2.22, 1.39 and 0.94 kW·m⁻² to 800, 750 and 700° C., respectively.

The proposal of this patent is based on the development of a catalyst and a ceramic anode electrocatalyst that have catalytic activity, electrocatalytic and electrochemical for the direct oxidation and/or internal reforming of ethanol and/or ethanol/water mixture, and may also allow to obtain C₂ hydrocarbons such as ethylene by dehydration of ethanol, and each reaction depends on the development of the catalyst by doping concentration and with different chemical elements, and the manufacturing process of the anode and the operating conditions of the fuel cell solid oxide, which includes concentration and pressure, relative fuel/oxidizer, and the ratio ethanol/water or the use of pure ethanol. Alternatively, in the Patent PI 0405676-0 A, Brazil (17, Oct. 2006 (RPI 1867) analyzes the use of electrocatalysts obtained by spontaneous deposition of platinum nanoparticles on Ru, Mn, Fe, Co, Rh, Pd, Os , Ir, Mo, Cr, V, W, Sn, U and rare earths, or a mixture of these elements, supported on carbon of high surface area, or by deposition of one or more of these elements on platinum nanoparticles supported on carbon of high surface area, as anode for the oxidation of alcohols, especially methanol and ethanol in the fuel cell electrolyte proton exchange membrane. This type of fuel cell, unlike SOFCs, operates at low temperatures and usually requires the use of noble metal electrocatalysts consisting of or containing in its composition, which is not required for the development of anodes for SOFCs due to its high operating temperature. For example, a key factor in obtaining special anodes for SOFCs is mainly the fabrication procedure that allows producing it as a component nanostructure. In the patent PI0601210-8, describes the procedures for the fabrication of nanostructured anodes for SOFCs. In another patent, PI0803895-3, is brought to life the composition and method of manufacture of anodes for SOFCs, also nanostructured, in which you can perform the direct oxidation of methane and methane-rich gas to produce electricity, but also for electrochemical conversion of methane to C₂ hydrocarbons, mainly ethylene, through reactions of direct oxidation of methane in the SOFC anode.

SUMMARY OF THE INVENTION

The main challenge for the direct oxidation and/or internal reform of ethanol to be commercially feasible in SOFC is to find efficient anodes electrocatalysts for the process of oxidation and that they can overcome all the constraints imposed by traditional Ni-anode ZEI. Find multifunctional anode electrocatalysts that are designed for specific functions, in addition to features already commonly required of an anode, which facility to include percolation of gases, and high catalytic activity in the electrocatalytic operating temperature and good electronic and ionic conductivities. These functions relate to specific features that can be of two types: 1) functionality related to materials and mechanical properties: type, quantity, distribution and stability of these phases and phases that may form in the manufacturing procedures and use; segregation and coalescence of particles and chemicals, mechanical stability, achieved by the production of anode layers with different compositions or through the use of materials on the anode and the electrolyte with coefficients of thermal expansion and contraction values close to, 2) catalytic functionality, electrochemical or electrocatalytic: resistance to selective deposition of carbon, which has the effect of disabling the electrocatalyst, competitive catalytic action, through chemical reactions that compete with the generation of electrons in electrochemical reactions, the degree of electrocatalytic activity, which influences the electrochemical performance. However, SOFC anodes can also be cross-functional, enabling the direct oxidation and/or internal reforming fuel complex, in addition to hydrogen, acting for the co-production of chemicals, to perform the electrochemical conversion of fuel in a chemical interest, in addition to co-produce electricity and heat.

The SOFCs are composed of clusters of low power battery unit. These groupings, in turn, can also be connected in series or in parallel to increase the installed power or the power generated. This feature provides great flexibility for scaling power and ease of maintenance of fuel cells. It is therefore object of the present invention to provide a process for the direct oxidation and/or internal reform of ethanol or ethanol/water mixture fuel cells using solid oxide, characterized in that it uses a fuel cell comprising a solid oxide anode multifunctional electrocatalyst composition-based mixed oxide and oxides of metals such as copper (CuO or Cu₂O), cerium (CeO₂), yttria stabilized zirconia (Zr₂O₃-Y₂O₃) and cerium aluminate (Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃), where M corresponds to an element among Sr and Ca, and x represents about a former content in the range 0 to 50 mol %, N corresponds to an element from among Mn, Cr, Co, and y is approximately in the range of content 0 to 50 mol %, the fuel cell is fed fuel complex mixtures such as ethanol or ethanol-water to produce electricity, heat, water and/or possibly through direct oxidation ethylene and/or internal reform.

In a preferred realization of the process, the liquid fuel supplied to the fuel cell is selected from ethanol, ethanol/water mixture or other alcohols.

In another embodiment of the preferred process, the fuel cell is operated at a temperature in the range 600 to 1000° C.

In another embodiment of the preferred process, the electric power is generated simultaneously by means of electrochemical conversion of chemical energy into electrical energy with high efficiency during the oxidation of ethanol produces 12 electrons per molecule and/or through internal reform.

In another embodiment of the preferred process, the fuel cell has high efficiency without the production of pollutants such as NO_(x) and SO_(x) and CO₂ emissions reduced.

In another embodiment of the preferred process, the fuel cell is operated with gas flow rates fuel/oxidant variables (0.5:1 to 3:1 and 2:1 to 1:3).

In another embodiment of the preferred process, the fuel cell is operated with fuel pre-heating.

In another embodiment of the preferred process, the fuel cell is operated with fuel vapor.

In another embodiment of the preferred process, the fuel cell is operated directly with a mixture of ethanol:water (mol) in a ratio ranging from 1:0 to 1:5.

In another embodiment of the preferred process, the fuel cell is operated with pure ethanol.

In another preferred realization of the process are preferably produced hydrocarbons such as ethylene, heat and electricity simultaneously through the association of ethanol and water.

It is also object of the present invention proposes a cell solid oxide fuel used for the direct oxidation and/or internal reform of ethanol and/or ethanol/water mixture, characterized by comprising an anode electrocatalyst with multifunctional chemical-based mixed oxides and oxides of metals such as copper (CuO and Cu₂O), cerium (CeO₂), Zr₂O₃-Y₂O₃ and cerium aluminate (Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃), where M corresponds to an element among Sr and Ca; x former represents about content in the range 0 to 50 mol %, N corresponds to an element among Mn, Cr, Co, and y represents approximately a content in the range 0 to 50 mol %, the stack is fed with fuel complex, such as ethanol and/or ethanol/water mixture to produce electricity, heat, water and/or possibly also by direct oxidation ethylene and/or internal reform.

In a preferred realization of the fuel cell, its functionality has gradually cathode made of a composite material La_(0.8)Sr_(0.2)MnO_(3+δ)/Zr₂O₃—Y₂O₃ (LSM/ZEI), the first layer consists of a functional film cathode of LSM/ZEI (20-50/80-50% by mass) and a second cathode LSM (La_(0.8)Sr_(0.2)MnO₃), and may have other compositions, and works with O₂ oxidants selected from air, pure O₂ or other gas mixtures O₂ and its rich electrolyte is ZEI (zirconia stabilized with 8 mol % yttria).

In a preferred realization of the fuel cell, it has at least one of the settings: supported by the electrolyte, the anode or the cathode.

In a preferred realization of the fuel cell, the electrolyte is conductive to oxygen O²⁻ions or protons, H⁺.

In a preferred realization of the fuel cell, not supported by the electrolyte, the electrolyte is presented in the form of a film, and the cell operated in a temperature range between 600 to 800° C.

In a preferred realization of the fuel cell, the anode presents electrochemical and electrocatalytic activity for oxidation of ethanol and ethanol-water mixtures.

In a preferred realization of the fuel cell, the anode provides catalytic function, electrocatalytic or electrochemical resistance to selective deposition of carbon.

In another preferred realization of the fuel cell, the anode multifunctional displays high electrochemical and electrocatalytic activity for the internal reforming of ethanol and ethanol-water mixtures.

In a preferred realization of the fuel cell, the anode multifunctional displays selectivity for the production of hydrocarbons such as ethylene.

It is also object of the present invention to provide a catalyst for the production of electricity from fuel ethanol used in fuel cell anodes of solid oxide, characterized by being made the basis of mixed oxides of cerium aluminate (Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃), where M corresponds to an element among Sr and Ca, and x represents about a content in the range 0 to 50 mol %, N corresponds to an element from among Mn, Cr, Co, and y represents approximately one in content range 0 to 50 mol %; active and selective in the direct oxidation and/or internal reform of ethanol and ethanol-water mixtures and provides a structure, preferably, the perovskite type.

In a preferred realization of the catalyst, it presents the range of thermal stability up to 1400° C.

In a preferred realization of the catalyst is synthesized with the same molar concentrations of Ce:Al in the range of from 1:1 to 2:3.

In a preferred realization of the catalyst, it presents both catalytic and electrocatalytic functions for generating electricity by direct oxidation of ethanol and ethanol-water mixtures.

In a preferred realization of the catalyst, it has high activity for the internal reform of ethanol and ethanol-water mixtures, and can convert up to 100% ethanol.

In a preferred realization of the catalyst with same features and characteristic of acidic sites due to the dehydration of ethanol to ethylene.

In a preferred realization of the catalyst, it has high activity attributed to its high capacity to adsorb ethanol.

In a preferred realization of the catalyst, it presents the electronic conductivity and activity for fuel oxidation.

DETAILED DESCRIPTION OF THE INVENTION

The present invention describes the use of fuel ethanol and ethanol-water mixtures in a reactor type solid oxide fuel cell—SOFC, with multifunctional electrocatalytic anode, the basis of oxides and mixed metal oxides with perovskite-type structure or not, to produce electricity, heat and chemicals.

For this purpose have been developed multifunctional anode electrocatalysts the basis of chemical composition of mixed oxides and oxides of metals such as copper (CuO and CuO₂), cerium (CeO₂), yttria stabilized zirconia (Zr₂O₃—Y₂O₃) and cerium aluminate (Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃), where M corresponds to an element among Sr and Ca, and x represents about a content in the range 0 to 50 mol %, N corresponds to an element from among Mn, Cr, Co, and y represents approximately a content in the range 0 to 50 mol %, the stack is fed with ethanol to produce electricity, heat, water and eventually ethylene by direct oxidation and/or internal reform of complex fuels such as ethanol or ethanol-water mixtures.

The following experimental procedures are described as an example of methodology that was used to obtain catalysts and manufacture of multifunctional SOFC anodes in order to promote the direct oxidation and/or internal reforming of ethanol or ethanol-water mixtures.

The catalysts with perovskite-type crystal structure were obtained from the decomposition of amorphous citrate were used as precursors of nitrate solutions. Initially, he prepared an aqueous solution was heated under magnetic stirring, until it was observed the formation of a highly viscous system. Then, citrate formed was dried in an oven, pre-calcined and subsequently calcined.

For the manufacture of ceramic suspensions for anodes multifunctional Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃—Zr₂O₃—Y₂O₃ the fuel cell unit solid oxide were used ZEI (zirconia stabilized with 8 mol % yttria) powders purchased commercially and Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃-synthesized powders.

Different ceramic suspensions were prepared, whose compositions suggested can be seen in Table 1. Each of them was used for the deposition of a functional component of the anode and has a specific function. The first component promotes better adhesion of the anode to the electrolyte, the second is the anode itself, which promotes the catalytic activity for fuel oxidation. The third component is not obtained from ceramic suspension, this is formed by impregnation of Cu nitrate and is added primarily to promote better electronic conduction in the anode, but also has the advantage of not contributing to promote the deposition of carbon.

TABLE 1 Functional Components of Anodes Component Anode Composition Function Functional 5-50% by weight of Promote better layer 1 Ce_(1-x)M_(x)Al_(1-y)N_(y)O₃/95-50% adhesion by weight of ZEI Functional Ce_(1-x)M_(x)Al_(1-y)N_(y)O₃ Anode layer 2 Element Copper Electronic impregnated conduction

For the preparation of a ceramic suspension, to create a functional layer, the powders Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃ and yttria-stabilized zirconia were thermally treated at temperatures in the range of 600-1000° C. and 700-1200° C., respectively. This initial heat treatment of powders is especially important to control the behavior of contraction that occurs during sintering, thus ensuring a better quality and reproducibility of the deposition and to control the particle size and distribution. Then, the powders were mixed, homogenized and heat treated.

Finally, the catalyst powder was mixed, a dispersant and a pore-forming ceramic suspension, added in proportions ranging from 5 to 60%. It generates a porous solid to facilitate the permeation of gases in the anode. Then the mixture was processed in a planetary ball mill (Retsch PM100) for the scattering of particles occurs by a mechanism of mechanical breakdown of the clusters.

In a subsequent step the suspension was prepared ceramic 2, to create the second functional layer, composed of only Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃. The suspension was prepared by adding the catalyst powder, dispersant and 5-60% of the suspension forming pores in the grinding vessel and grinding media.

For the preparation of the anode, the ceramic suspensions were deposited by screen printing on the electrolyte of stabilized zirconia with 8 mol % yttria was deposited layer by layer. We first made the deposition of a layer using a ceramic suspension 1 then were deposited layer with the ceramic suspension 2. After that, the deposition was followed by a sintering heat treatment levels and rates of heating and cooling according to each specific catalytic material, resulting in a porous anode.

Subsequent to the step of sintering the porous anode was placed the third component of the anode, processed through the impregnation of copper nitrate. Cu salts were added to the anode using a series of steps of impregnation of an aqueous solution of copper nitrate (Cu(NO₃)_(2.3)H₂O) until the desired concentration. After each impregnation with copper nitrate, the anode passed through the drying process. Under these conditions the deposited copper salts were converted to copper oxides and reduced to metallic Cu on activation of SOFC under hydrogen atmosphere.

It experienced the manufacture of anodes containing the multifunctional components 1 and 2 described above with different thicknesses ranging from 10 to 600 μm, and repeating alternating deposition of these components before impregnation with the third component, composed of copper.

On the other side of the electrolyte was applied by screen printing functionality to the cathode gradually La_(0.8)Sr_(0.2)MnO_(3+δ)/Zr₂O₃—Y₂O₃ (LSM/ZEI), the first layer consists of a functional film cathode LSM/ZEI (20-50/80-50% by mass) and a second cathode LSM (La_(0.8)Sr_(0.2)MnO₃), or any other composition of the cathode. Being sintered and then composing this way the combined electrode/electrolyte of a SOFC unit. For the collection of current in the anode and cathode wires were used for platinum and gold respectively.

The anode of the battery unit La_(0.8)Sr_(0.2)MnO_(3+δ)—Zr₂O₃—Y₂O₃/Zr₂O₃—Y₂O₃/Cu—Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃—Zr₂O₃—Y₂O₃ were reduced in H₂ atmosphere for a few hours prior to testing of SOFCs. To avoid the sintering of copper and maintain the electrochemical performance of anode functional tests were performed at temperatures between 600-950° C. Pure ethanol, hydrogen and mixtures of ethanol/water were used as fuels and oxidants were selected from air O₂ and pure O₂. The liquid fuel, ethanol was added to the system through a saturator and vaporized by using a thermostatic bath, being led by the carrier gas, nitrogen, until the surface of the anode multifunctional. It is worth mentioning that, under the reducing atmosphere during fuel cell operation, the main active component of multifunctional electrocatalytic anode is the lanthanum aluminate (Cu—Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃ as described above). This becomes reversibly phases CeO₂ and γ-Al₂O₃ in an oxidizing atmosphere, outside the operating conditions of the fuel cell.

EXAMPLES Example 1

This example shows the characteristics of the catalyst based on cerium aluminate (Cu—Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃), where M corresponds to an element among Sr and Ca, and x represents about a content in the range 0 to 50 mol %, N corresponds to an element from among Mn, Cr, Co, and y represents approximately a content in the range 0 to 50 mol %. In this work the least amount of surface area found for the catalyst under study was 16.72 m²·g⁻¹, when heat treated at 900° C. This value rises as the annealing temperature decreases and increases with increasing content of doping. These results are consistent with the average particle size, whereas the surface area decreases and the particle size increases with increasing annealing temperature. This observation may be related to the union between the particles for possible mass transfer of the material in question. The particle size distribution for the systems studied showed distribution bi and Trimode. This fact indicates the presence of clusters, with an open distribution. FIGS. 1 (a) to 1 (d) shows the micrographs of the catalyst powder particles obtained by scanning electron microscopy, to ascertain the distribution of particles with a few clusters.

Example 2

This example demonstrates the influence of the manufacturing process on the microstructure of the anode multifunctional electrocatalyzer the basis of chemical composition of mixed oxides and oxides of metals such as copper (CuO and Cu₂O), cerium (CeO₂), yttria stabilized zirconia (Zr₂O₃—Y₂O₃) and cerium aluminate (Cu—Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃), where M corresponds to an element among Sr and Ca, and x represents about a content in the range 0 to 50 mol %, N corresponds to an element from among Mn, Cr, Co, and y represents approximately a content in the range 0 to 50 mol %. FIGS. 2 (a) and 2 (b) show the microstructure of the anode porous cerium aluminate (Cu—Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃) sintered before impregnation with Cu. There is a significant amount of pores, resulting from the pyrolysis of ceramic suspension forming pores. It is also observed the formation of regions of high porosity throughout the sample, given that the micrographs show different regions of the same ceramic body, and the pores have approximately spherical shape, characterizing the shape of the pore-forming element. The impregnation with copper nitrate solution (Cu(NO₃)_(2.3)H₂O) on the porous anode produced a relatively large amount of Cu oxide precipitates probably formed during the evaporation of water during the drying process. The size and shape of the Cu oxide deposits depend on the size of the droplets of the solution during drying, resulting in particles of copper oxide, as shown in FIGS. 2 (c) and 2 (d). The precipitates were subsequently reduced to Cu metal in the operating conditions of SOFCs.

Example 3

In the test conducted with the electrochemical performance SOFCs La_(0.8)Sr_(0.2)MnO_(3+δ)—Zr₂O₃—Y₂O₃/Zr₂O₃—Y₂O₃/Cu—Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃—Zr₂O₃—Y₂O₃, where M corresponds to an element among Sr and Ca, and x represents approximately a content in the range 0 to 50 mol %, N corresponds to an element among Mn, Cr, Co, and y represents approximately a content in the range 0 to 50 mol %. The fuel cell unit supported by an electrolyte with a thickness of 200 μm was efficient in generating electricity directly when operated with hydrogen or ethanol or ethanol-water mixtures, FIGS. 3 (a) and 3 (b), respectively. As expected, better results were obtained for operation with H₂, however, the performance of SOFCs operated with C₂H₅OH was very significant given that there was no carbon deposit on the anode electrocatalyst.

This leads to the conclusion that the tested SOFCs have a view to presenting long life with good performance during its operation with direct feed from ethanol or ethanol-water mixtures. This characterizes the components as strong candidates for direct oxidation of ethanol and hydrocarbons. The reduction in current density of SOFC operated with direct ethanol in relation to the SOFC operated with hydrogen can be related to greater weight of ethanol molecules, which induces slower diffusion of the fuel gas, increasing the concentration polarization. In addition, more complex electrochemical reactions take place at the anode of the fuel cell directly fed with ethanol. 

1. Process for the direct oxidation and / or internal reform of ethanol fuel cells using solid oxide, characterized by the fact that it uses a fuel cell comprising a solid oxide anode electrocatalyst multifunctional chemical-based mixed oxides and metal oxides such as copper (CuO and Cu₂O), cerium (CeO₂), yttria stabilized zirconia (Zr₂O₃—Y₂O₃) and cerium aluminate (Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃), where M corresponds to an element among Sr and Ca; and x represents approximately a content in the range 0 to 50 mol %, N corresponds to an element from among Mn, Cr, Co, and y represents approximately a content in the range 0 to 50 mol %, the stack is fed with fuel complex such as ethanol or ethanol-water mixtures, to produce electricity, heat, water and/or possibly through direct oxidation ethylene and/or internal reform.
 2. Process according to claim 1, characterized by the fact that the liquid fuel supplied to the fuel cell is selected from ethanol, ethanol/water mixture or other alcohols.
 3. Process according to claim 1, characterized by the fact that the fuel cell is operated at a temperature ranging from 600 to 1000° C.
 4. Process according to claim 1, characterized by the fact that the fuel ethanol is oxidized directly or retired directly into the anode cell.
 5. Process according to claim 1, characterized by the fact that the fuel cell is operated with gas flow rates fuel/oxidant variables (0.5:1 to 3:1 and 2:1 to 1:3).
 6. Process according to claim 1, characterized by the fact that the electricity is generated simultaneously by means of electrochemical conversion of chemical energy into electrical energy with high efficiency during the oxidation of ethanol, producing 12 electrons of energy per mole of ethanol.
 7. Process according to claim 1, characterized by the fact that the fuel cell has high efficiency without the production of pollutants such as NO_(x) and SO_(x) and CO₂ emissions reduced.
 8. Process according to claim 1, characterized by the fact that the fuel cell is operated with fuel vaporized and preheated.
 9. Process according to claim 1, characterized by the fact that the fuel cell is operated when the fuel at room temperature to be introduced into the fuel cell solid oxide.
 10. Process according to claim 1, characterized by the fact that the fuel cell to be operated directly with an ethanol/water mixture (mol) in a ratio ranging from 1:0 to 1:5.
 11. Process according to claim 10, characterized by the fact that the fuel cell to produce hydrogen instead, both through the association of ethanol and water.
 12. Process according to claim 1, characterized by the fact that the fuel cell to produce preferably hydrocarbons such as ethylene by dehydration of ethanol.
 13. Stack solid oxide fuel used for the direct oxidation and/or internal reform of fuel, characterized by the fact that comprising an anode electrocatalyst with multifunctional chemical-based mixed oxides and metal oxides such as copper (CuO and Cu₂O), cerium (CeO₂), Zr₂O₃—Y₂O₃ and cerium aluminate (Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃), where M corresponds to an element among Sr and Ca, and x represents about a content in the range 0 to 50 mol %, N corresponds to an element from among Mn, Cr, Co, and y represents approximately a content in the range 0 to 50 mol %.
 14. Fuel cell according to claim 13, characterized by the fact that the composition has its cathode La_(0.8)Sr_(0.2)MnO_(3+δ/Zr) ₂O₃—Y₂O₃ (LSM/ZEI), the first layer consists of a film cathode LSM/ZEI (20-50/80-50% by mass) and a second cathode LSM (La_(0.8)Sr_(0.2)MnO₃) or other cathodes, and operates with O₂ oxidants selected from air, pure O₂ or other gas mixtures rich in O₂ and its electrolyte is ZEI (zirconia stabilized with 8% yttria) or other ceramic ionic conductor and impermeable to gas.
 15. Fuel cell in accordance to claim 13, characterized by the fact that having at least one of the settings: supported by the electrolyte, the anode or the cathode.
 16. Fuel cell according to claim 13, characterized by the fact that the electrolyte is conductive to oxygen O²⁻ ions or protons, H⁺.
 17. Fuel cell according to claim 13, not supported by the electrolyte, characterized in that the electrolyte is presented in the form of film and the cell operated at temperatures of 600 to 800° C.
 18. Fuel cell according to claim 13, characterized in that the supporting electrolyte is presented on the electrodes or electrode layer deposited on the substrate, the cell operated at temperatures from 700 to 1000° C.
 19. Fuel cell according to claim 13, characterized by the fact that the anode presents electrochemical and electrocatalytic activity for oxidation of ethanol.
 20. Fuel cell according to claim 13, characterized by the fact that the anode has multifunctional catalytic, electrocatalytic and electrochemical, are still able to limit the deposition of carbon.
 21. Fuel cell according to claim 13, characterized by the fact that the anode multifunctional has high electrochemical and electrocatalytic activity for the internal reform of ethanol.
 22. Fuel cell according to claim 21, characterized by characterized by the fact that the anode multifunctional displays selectivity for the production of hydrocarbons such as ethylene.
 23. Fuel cell according to claim 22, characterized by the fact that it is directly fed with ethanol and/or ethanol/water mixture, with outputs in the range of Watts, or kWatts mWatts for distributed generation of electricity in remote locations, disconnected from the national grid power.
 24. Fuel cell according to claim 23, characterized by the fact that it is directly fed with ethanol and/or ethanol/water mixture, with outputs in the range of Watts, or kWatts mWatts for distributed generation of electricity in sites connected to the national grid electricity.
 25. Fuel cell according to claim 24, characterized by the fact that supply electricity to local devices, stationary systems and also to the national grid power when the demand for such local devices and stationary systems is less their ability to produce electricity.
 26. Fuel cell according to claim 25, characterized by the fact that having their applications targeted for use in homes, offices, businesses, schools, hospitals and the like, for providing electrical energy to power and heat for local heating water and space heating.
 27. Fuel cell according to claim 26, characterized by the fact that the heat produced is used for cogeneration, allowing the production of electricity in addition to that produced by the fuel cell, can also be used for space heating, heat water, generate steam and heat other equipment, including reformers.
 28. Fuel cell according to claim 27, characterized by the fact that its use aimed at mobile and portable devices such as games, computers, cell phones, PDAs, notebooks, laptops and other devices generally powered by batteries or conventional batteries.
 29. Fuel cell according to claim 28, characterized by the fact that having their applications focused on vehicles, acting as an auxiliary power unit.
 30. Characterized fuel cell according to claim 29, characterized by the fact that it is applied in the generation of electricity in hybrid electric vehicles or not, for the traction system of vehicles and can be applied in automobiles, buses, trucks, trains, motorcycles and special-purpose vehicles such as forklifts, golf carts, among others.
 31. Catalyst for production of electricity from fuel ethanol and/or ethanol/water mixture used in fuel cell anodes of solid oxide, characterized by the fact that being made the basis of mixed oxides of cerium aluminate (Ce_(1−x)M_(x)Al_(1−y)N_(y)O₃), where M corresponds to an element among Sr and Ca, and x represents about a content in the range 0 to 50 mol %, N corresponds to an element from among Mn, Cr, Co, and y represents approximately one in content range 0 to 50 mol %; active and selective in the direct oxidation and/or internal reform of ethanol and has a structure, preferably, the perovskite type.
 32. Catalyst according to claim 31, characterized by the fact that present in the range of thermal stability up to 1400° C.
 33. Catalyst according to claim 31, characterized by the fact that it is synthesized with molar concentrations of Ce:Al in the range of from 1:1 to 2:3.
 34. Catalyst according to claim 31, characterized by the fact that simultaneously display catalytic and electrocatalytic functions for generating electricity by direct oxidation of ethanol and/or mixtures of ethanol/water.
 35. Catalyst according to claim 31, characterized by the fact that it shows high activity for the internal reform of ethanol and/or mixtures of ethanol/water, with conversion of up to 100% ethanol.
 36. Catalyst according to claim 31, characterized by the fact that the acid sites have characteristic, favoring the dehydration of ethanol to ethylene.
 37. Catalyst according to claim 31, characterized by the fact that it shows high activity attributed to its high capacity to adsorb ethanol.
 38. Catalyst according to claim 31, characterized by the fact that the catalytic and electrocatalytic functions provide the selectivity for ethylene production of hydrocarbons.
 39. Catalyst according to claim 31, characterized by the fact that a reversible transformation of phases such that, when out of operation is composed primarily of CeO₂ and γ-Al₂O₃ and when in operation is constituted mainly by cerium aluminates.
 40. Catalyst according to claim 39, characterized by presents perovskite structure in a reducing atmosphere under operating conditions the fuel cell.
 41. Catalyst according to claim 39, characterized by the fact that the phases present CeO₂ and γ-Al₂O₃ in an oxidizing atmosphere. 